In-situ activation integrated treatment device for biomass hydrogenation catalyst
By adopting a coaxial nested riser and central return gas pipe structure, as well as a mixing intake chamber and baffle design in the biomass hydrogenation reactor, the problems of heat management and catalyst circulation were solved, achieving efficient thermal coupling and catalyst regeneration, and improving the stability and economy of the reactor.
Patent Information
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- NINGBO UNIVERSITY OF TECHNOLOGY
- Filing Date
- 2026-05-07
- Publication Date
- 2026-07-03
AI Technical Summary
Existing fluidized bed reactors in biomass hydrogenation processes suffer from uneven heat management, catalyst cycling dependence on easily worn mechanical parts, and difficulty in integrating catalyst regeneration and reaction separation, resulting in low thermal energy utilization, high equipment costs, and poor stability.
The reactor employs a coaxial nested riser and central return pipe structure, combined with a mixing intake chamber and baffle design, to achieve thermal coupling and in-situ activation of the catalyst inside the reactor, simplifying the catalyst circulation and regeneration process, and integrating gas-solid mixing and regeneration functions into one.
It improves thermal energy utilization, reduces equipment dependence on external heating sources, simplifies mechanical parts, enhances reaction efficiency and equipment stability, and reduces investment and land costs.
Smart Images
Figure CN122321739A_ABST
Abstract
Description
Technical Field
[0001] This invention relates to the field of biomass energy chemical technology, specifically to an integrated in-situ activation treatment device for biomass hydrogenation catalysts. Background Technology
[0002] Biomass catalytic hydrogenation technology is an important pathway for converting renewable biomass resources into high-value-added liquid fuels or chemicals. In this process, the catalyst plays a crucial role. However, due to the complex composition of biomass feedstocks, coke or heavy polymers are easily deposited on the catalyst surface during the reaction, leading to the covering of active sites and rapid deactivation. Therefore, achieving efficient catalyst recycling, heat balance, and activity maintenance are key to the industrial application of this technology.
[0003] Although existing fluidized bed reactors or circulating fluidized bed (CFB) technologies have been widely used in gas-solid catalytic reaction processes, they still have significant limitations when handling specific processes such as biomass hydrogenation. In terms of heat management, biomass hydrogenation processes typically require strict temperature control, but traditional fluidized bed reactors often lack efficient internal thermal coupling mechanisms. The isolation between the reaction zone and the heating zone leads to large radial or axial temperature differences within the reactor, and excessive reliance on external heating equipment to preheat feedstocks or maintain reaction temperatures results in low energy efficiency and poor product selectivity.
[0004] Regarding catalyst circulation and transport, existing technologies often employ complex external circulation pipeline systems. This involves using independent downcomers, risers, and mechanical control components such as slide valves and plug valves to regulate catalyst flow between the reactor and regenerator. These mechanical moving parts are constantly exposed to high-temperature, high-wear gas-solid flow fields, making them highly susceptible to wear, jamming, and even failure. This not only increases the manufacturing and maintenance costs of the equipment but also severely impacts the stability of long-term operation. Furthermore, relying on mechanical transport makes it difficult to achieve instantaneous micro-mixing of the gas and solid phases before they enter the reaction zone, affecting mass transfer efficiency.
[0005] Furthermore, in catalyst regeneration, traditional processes typically separate the reaction and regeneration processes completely, requiring large, independent regenerators and associated pipelines, resulting in large plant footprints and high investment costs. Meanwhile, technologies for directly treating the catalyst inside the reactor are relatively scarce. Existing reactor structures struggle to utilize the high-temperature product gases generated by the reaction itself for in-situ stripping and preliminary activation of the settled catalyst. This makes it difficult to effectively address the issues of slight coking and heavy component adsorption on the catalyst surface within a compact space, necessitating frequent catalyst extraction for deep regeneration, thus reducing process continuity and economic efficiency. Summary of the Invention
[0006] To address the shortcomings of existing technologies, this invention provides an integrated in-situ activation and regeneration device for biomass hydrogenation catalysts. This device solves the problems of low thermal energy utilization due to the lack of an efficient thermal coupling mechanism within existing fluidized bed reactors, high dependence on easily worn external mechanical parts for catalyst circulation and transportation, and difficulty in simultaneously achieving efficient gas-solid mixing and in-situ catalyst activation and regeneration within a compact single unit.
[0007] To achieve the above objectives, the present invention is implemented through the following technical solution: an integrated in-situ activation treatment device for biomass hydrogenation catalyst, comprising: a reactor body, a reflux assembly, a feed assembly, a gas-solid separation assembly, and an annular activation zone located inside the reactor body; The reactor body includes a reactor shell, and a top cover and a bottom cover respectively sealed to the top and bottom of the reactor shell. The reflux assembly is disposed inside the reactor shell. The feeding assembly is disposed at the bottom end cap and includes a feeding pipe passing through the bottom end cap and a nozzle connected to the end of the feeding pipe. The feeding assembly also includes a mixing suction chamber covering the nozzle. The reflux assembly includes a riser pipe vertically disposed at the central axis of the reactor shell, and a central return gas pipe coaxially sleeved inside the riser pipe. The bottom end of the riser pipe is connected to the mixing and suction chamber, and an annular activation zone is formed between the outer wall of the riser pipe and the inner wall of the reactor shell. The gas-solid separation assembly includes a cyclone separator eccentrically positioned at the top of the reactor body. The cyclone separator has a tangential inlet that communicates with the gas phase space above the riser.
[0008] Preferably, the reactor body further includes a settling section disposed on the upper part of the reactor shell, the diameter of the settling section being larger than the diameter of the lower part of the reactor shell, and an exhaust pipe connected to the top of the top cover, the exhaust pipe being connected to the gas-solid separation component.
[0009] Preferably, the mixing and inhalation chamber has an inverted trumpet-shaped or cylindrical structure, and the bottom of the mixing and inhalation chamber is connected to several supporting legs, which support the top of the bottom end cap, so that an inhalation gap for the catalyst to pass through is formed between the bottom edge of the mixing and inhalation chamber and the bottom end cap.
[0010] Preferably, the reflux assembly further includes several positioning ribs connected between the inner wall of the riser pipe and the outer wall of the central return gas pipe, the central return gas pipe being used to transport the gas from the upper part of the reactor downward to the mixing and inhalation chamber.
[0011] Preferably, the reflux assembly further includes a reflux gas collection hood disposed above the outlet of the riser pipe. The reflux gas collection hood is in the shape of an inverted funnel, and its lower end is sealed to the upper opening of the central reflux pipe.
[0012] Preferably, the reflux assembly further includes a filter screen covering the upper opening of the reflux gas collection hood for filtering the gas entering the central reflux pipe.
[0013] Preferably, the cyclone separator is provided with an air riser at the top, which is connected to the exhaust pipe, and the bottom of the cyclone separator is connected to a downwardly extending material leg.
[0014] Preferably, a one-way valve is provided at the end of the material leg, and the one-way valve is configured to prevent gas in the annular activation zone from flowing back into the cyclone separator.
[0015] Preferably, the annular activation zone is provided with baffles, which are staggered and fixed to the inner wall of the reactor shell and the outer wall of the riser.
[0016] An integrated in-situ activation method for biomass hydrogenation catalysts includes the following steps: S1 Raw Material Injection and Mixing: The biomass raw material is fed through the feed pipe of the feeding assembly to the nozzle and sprayed upward. A negative pressure is formed in the mixing and suction chamber, and the catalyst outside the mixing and suction chamber is drawn in through the gap between the support legs. The drawn-in catalyst, raw material and high-temperature return gas from the central return gas pipe are mixed to form a gas-solid mixture. S2 reaction and heat exchange: The gas-solid mixture flows upward into the riser of the reflux assembly and undergoes a hydrogenation reaction. At the same time, the high-temperature reflux gas flows downward in the central return gas pipe and transfers heat to the fluid in the riser through the pipe wall. S3 Gas-Solid Separation: The gas-solid mixture after the reaction undergoes initial settling in the settling section, and then enters the cyclone separator of the gas-solid separation component. The separated gas flows into the exhaust pipe through the riser pipe and is discharged. The separated catalyst falls back through the material leg opening the one-way valve. S4 In-situ Activation and Regeneration: The catalyst is brought back to the annular activation zone. During the fall, it is disturbed by the baffle plate and stripped by the countercurrent upward gas in the annular activation zone. After completing the in-situ activation, it settles to the bottom and participates in the cycle of step one again. S5 Gas Reflux Circulation: A portion of the high-temperature product gas is captured by the reflux gas collection hood. After being filtered by the filter screen, the gas enters the central return gas pipe and flows downwards.
[0017] This invention provides an integrated in-situ activation device for biomass hydrogenation catalysts. It offers the following advantages: 1. This invention, by setting up a coaxial nested riser and central return gas pipe structure, uses the central return gas pipe to return the high-temperature gas at the top downwards, so that the high-temperature return gas can directly provide heat to the endothermic hydrogenation reaction inside the riser through the pipe wall, realizing thermal coupling inside the reactor. This not only reduces the device's dependence on external heating sources, but also effectively maintains the uniformity and stability of the temperature field inside the riser, avoiding catalyst deactivation caused by local temperature differences.
[0018] 2. The present invention adopts a mixing and suction chamber based on the Venturi effect and a suspended support leg structure at the bottom. By utilizing the negative pressure generated by the high-speed injection of raw materials, the catalyst to be generated is automatically drawn into the riser pipe directly through the bottom gap without the need for additional mechanical conveying equipment. This gas-solid contact method not only simplifies the equipment structure and reduces the failure rate, but also uses strong turbulence to achieve instantaneous uniform mixing of raw materials and catalysts before entering the reaction zone, thereby improving the reaction efficiency.
[0019] 3. This invention utilizes the annular gap between the riser and the reactor shell to construct an annular activation zone with baffles. The baffles extend the catalyst's falling path and residence time, and the high-temperature product gas flowing counter-currently upwards is used to strip and purge the catalyst surface. The reaction, separation, and regeneration functions are integrated into the same reactor shell. Without the need for a separate regenerator, the removal of slight carbon deposits on the catalyst surface and the restoration of its activity can be completed, significantly reducing equipment investment and floor space requirements. Attached Figure Description
[0020] Figure 1 This is a perspective view of the present invention; Figure 2 This is a cross-sectional view of the reactor body of the present invention; Figure 3 This is a schematic diagram of the recirculation component of the present invention; Figure 4 This is a schematic diagram of the gas-solid separation component of the present invention; Figure 5 This is a schematic diagram of the feeding assembly of the present invention; Figure 6 for Figure 3 Enlarged view of point A in the middle; Figure 7 This is a flowchart of the method steps of the present invention.
[0021] The components include: 1. Reactor body; 101. Reactor shell; 102. Settling section; 103. Top cover; 104. Bottom end cap; 105. Exhaust pipe; 2. Reflux assembly; 201. Lifting pipe; 202. Central return gas pipe; 203. Positioning ribs; 204. Reflux gas collection hood; 205. Filter screen; 3. Feed assembly; 301. Mixing suction chamber; 302. Support leg; 303. Feed pipe; 304. Nozzle; 4. Gas-solid separation assembly; 401. Cyclone separator; 402. Lifting pipe; 403. Material leg; 404. One-way valve; 5. Annular activation zone; 6. Baffle plate. Detailed Implementation
[0022] The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. Based on the embodiments of the present invention, all other embodiments obtained by those skilled in the art without creative effort are within the scope of protection of the present invention.
[0023] Please see the appendix Figure 1 -Appendix Figure 7 This invention provides an integrated in-situ activation treatment device for biomass hydrogenation catalysts, comprising a reactor body 1, a reflux assembly 2 disposed inside the reactor, a feed assembly 3 located at the bottom, a gas-solid separation assembly 4 located at the top, and an annular activation zone 5 located inside the reactor body 1. The reactor body 1 serves as a pressure vessel, consisting of a cylindrical reactor shell 101 and a top cover 103 and a bottom cover 104 respectively sealed and connected to the top and bottom ends of the shell. The material is typically high-temperature and high-pressure resistant alloy steel to adapt to the hydrogenation environment. In the upper part of the reactor shell 101, corresponding to the area above the outlet of the riser pipe 201, a settling section 102 with an enlarged diameter is provided. The diameter of the settling section 102 is larger than the diameter of the lower reactor shell 101, which aims to reduce the upward velocity of the gas flow to promote the gravity settling of large catalyst particles. An exhaust pipe 105 is connected to the highest point of the top cover 103, serving as the final gaseous product outlet of the device. The exhaust pipe 105 is connected to the internal gas-solid separation assembly 4.
[0024] The reflux assembly 2 is vertically positioned at the center of the reactor shell 101. This assembly adopts a coaxial sleeve structure, including a riser pipe 201 as the main reaction channel and a central return gas pipe 202 as the heat source reflux channel. The riser pipe 201 is vertically positioned at the central axis of the reactor, and its outer wall forms an annular activation zone 5 between the inner wall of the reactor shell 101 and the outer wall of the reactor shell 101. The central return gas pipe 202 is coaxially sleeved inside the riser pipe 201. To ensure the coaxiality of the two and enhance the structural rigidity, several positioning ribs 203 are axially connected between the inner wall of the riser pipe 201 and the outer wall of the central return gas pipe 202. This allows the central return gas pipe 202 to not only transport the hot gas from the upper part of the reactor downward to the mixing and suction chamber 301 at the bottom, but also to directly transfer heat to the reaction fluid inside the riser pipe 201 through the pipe wall, thus achieving internal heat coupling. In addition, a funnel-shaped return gas collection hood 204 is provided above the outlet of the riser pipe 201. Its lower end is sealed to the upper opening of the central return gas pipe 202 to capture the rising hot gas flow. In order to prevent solid particles from clogging the internal pipe, a filter screen 205 is also covered at the upper opening of the return gas collection hood 204 to filter out large particulate impurities before the gas enters the central return gas pipe 202.
[0025] The feed pipe 303 is vertically inserted into the bottom of the reactor, and its end is connected to an upward spray nozzle 304. An inverted trumpet-shaped or cylindrical mixing suction chamber 301 is provided above the nozzle 304. The upper part of the mixing suction chamber 301 is connected to the bottom end of the riser pipe 201. The mixing suction chamber 301 is not directly welded to the bottom head 104, but is supported on the top of the bottom head 104 by several support legs 302, thereby forming a suction gap between the bottom edge of the mixing suction chamber 301 and the bottom head 104. When the raw material is sprayed out at high speed through the nozzle 304, a Venturi negative pressure effect will be generated in the mixing suction chamber 301, thereby driving the external catalyst to enter the mixing zone through the above-mentioned suction gap and mix with the raw material and the return gas from the central return gas pipe 202.
[0026] The gas-solid separation assembly 4 includes a cyclone separator 401 eccentrically positioned at the top of the reactor body 1. The cyclone separator 401 has a tangential inlet that is horizontally aligned with the gas phase space above the riser 201 to receive the gas-solid mixture flowing out of the riser 201. The riser 402 at the top of the cyclone separator 401 passes upward through the top cover 103 and merges into the exhaust pipe 105 to discharge the purified gas. Its bottom is connected to a downwardly extending slender material leg 403. The end of the material leg 403 is inserted into the lower part of the annular activation zone 5. In order to prevent gas backflow from disrupting the flow field of the cyclone separator 401, a one-way valve 404 is also provided at the end of the material leg 403. The one-way valve 404 is configured to open only when sufficient material column pressure accumulates in the material leg 403 to prevent gas backflow in the annular activation zone 5.
[0027] In addition, in order to achieve online regeneration and activation of the catalyst, several baffles 6 are fixed alternately in the annular activation zone 5 between the riser 201 and the reactor shell 101. These baffles 6 are respectively connected to the inner wall of the reactor shell 101 or the outer wall of the riser 201 to block the straight settling of the catalyst, making its falling path tortuous, thereby increasing the residence time of the catalyst in the hydrogen-rich environment, and using the countercurrent upward hot gas flow to strip and purge the catalyst surface.
[0028] This invention also provides an integrated in-situ activation method for biomass hydrogenation catalysts, comprising the following steps: S1 Raw material injection and mixing: The biomass raw material is brought to the nozzle 304 through the feed pipe 303 of the feed assembly 3 and sprayed upward. A negative pressure is formed in the mixing and suction chamber 301, and the catalyst outside the mixing and suction chamber 301 is sucked in through the gap between the support legs 302. The sucked-in catalyst, raw material and high temperature return gas from the central return gas pipe 202 are mixed to form a gas-solid mixture. S2 reaction and heat exchange: The gas-solid mixture flows upward into the riser 201 of the reflux assembly 2 and undergoes a hydrogenation reaction. At the same time, the high-temperature reflux gas flows downward in the central return gas pipe 202 and transfers heat to the fluid in the riser 201 through the pipe wall. S3 Gas-solid separation: The gas-solid mixture after the reaction undergoes initial settling in the settling section 102, and then enters the cyclone separator 401 of the gas-solid separation component 4. The separated gas flows into the exhaust pipe 105 through the riser pipe 402 and is discharged. The separated catalyst falls back through the material leg 403 opening the one-way valve 404. S4 In-situ activation and regeneration: The catalyst falls back to the annular activation zone 5. During the fall, it is disturbed by the baffle plate 6 and stripped by the countercurrent upward gas in the annular activation zone 5. After completing the in-situ activation, it settles to the bottom and participates in the cycle of step one again. S5 Gas Reflux Circulation: Part of the high-temperature product gas is captured by the reflux gas collection hood 204. After being filtered by the filter screen 205, the gas enters the central return gas pipe 202 and flows downward.
[0029] Working principle: When using this equipment, biomass feedstock enters the device through the bottom feed pipe 303 and is ejected upwards at high speed through the nozzle 304. The high-speed fluid forms a local negative pressure zone inside the mixing and suction chamber 301. Under the action of pressure difference, the regenerated catalyst accumulated outside the mixing and suction chamber 301 is entrained into the mixing and suction chamber 301 through the gap between the support leg 302 and the bottom end cap 104. The feedstock fluid, the high-temperature return gas flowing out from the central return gas pipe 202, and the sucked-in catalyst complete preliminary turbulent mixing and heat exchange in the mixing and suction chamber 301, forming a gas-solid mixed flow. The gas-solid mixture then enters the riser 201. During the upward flow, the raw material and the active sites on the catalyst surface come into full contact and undergo a hydrogenation reaction. At the same time, the high-temperature return gas flows downward through the central return gas pipe 202 nested inside the riser 201. Since the riser 201 and the central return gas pipe 202 are connected by positioning ribs 203 and coaxially sleeved, the heat in the central return gas pipe 202 can be directly transferred to the reaction fluid in the riser 201 through the pipe wall. This not only maintains the reaction temperature in the riser 201, but also achieves internal self-balance of the reaction heat. After the gas-solid mixture from the reaction exits the top of the riser 201, it enters the settling section 102 with an enlarged diameter. Due to the sudden increase in the flow cross-sectional area, the gas velocity decreases, and large catalyst particles naturally settle and separate under gravity. The product gas stream carrying fine catalyst powder enters the cyclone separator 401 tangentially after being deflected. Under centrifugal force, the solid catalyst particles are thrown against the wall and slide down to the bottom feed leg 403. After accumulating to a certain weight, they push open the one-way valve 404 and fall back to the lower bed. The purified product gas then flows through the riser 402 into the exhaust pipe 105 and is finally discharged from the reactor body 1 to enter the subsequent condensation section. The separated catalyst falls back into the annular activation zone 5 between the reactor shell 101 and the riser 201. Under the influence of gravity, the catalyst moves slowly downward in a dense bed. During this process, the catalyst particles collide and slide with the baffles 6 set in the annular gap, making the falling path tortuous and thus prolonging the residence time. At the same time, some of the high-temperature product gas that is not captured by the return gas collection hood 204 diffuses upward in the annular activation zone 5, stripping and purging the catalyst falling along the way, desorbing the heavy components and carbon precursors adsorbed on the catalyst surface. After stripping and regeneration activation, the catalyst finally settles to the bottom of the reactor and is drawn back in by the negative pressure at the bottom of the mixing and suction chamber 301, completing the entire catalyst recycling and regeneration process. In the gas phase space of the settling section 102, the reflux gas collection hood 204 actively captures part of the high-temperature product gas by using the ejector negative pressure at the bottom of the central return gas pipe 202. After the gas passes through the filter screen 205 to remove large particulate impurities, it enters the central return gas pipe 202 and is transported downwards, returning to the bottom of the reactor to participate in the preheating of raw materials and the fluidization of catalyst, thus realizing a closed-loop circulation of heat and medium.
Claims
1. An integrated in-situ activation treatment device for biomass hydrogenation catalysts, characterized in that, include: The reactor body (1), reflux assembly (2), feed assembly (3), gas-solid separation assembly (4) and an annular activation zone (5) located inside the reactor body (1); The reactor body (1) includes a reactor shell (101), and a top cover (103) and a bottom cover (104) respectively sealed and connected to the top of the reactor shell (101) and the bottom. The reflux assembly (2) is disposed inside the reactor shell (101). The feeding assembly (3) is disposed at the bottom end cap (104), and includes a feeding pipe (303) passing through the bottom end cap (104) and a nozzle (304) connected to the end of the feeding pipe (303). The feeding assembly (3) also includes a mixing suction chamber (301) covering the nozzle (304). The reflux assembly (2) includes a riser pipe (201) vertically disposed at the central axis of the reactor shell (101) and a central return gas pipe (202) coaxially sleeved inside the riser pipe (201). The bottom end of the riser pipe (201) is connected to the mixing and suction chamber (301). An annular activation zone (5) is formed between the outer wall of the riser pipe (201) and the inner wall of the reactor shell (101). The gas-solid separation assembly (4) includes a cyclone separator (401) eccentrically disposed on the top of the reactor body (1), the cyclone separator (401) having a tangential inlet and the tangential inlet communicating with the gas phase space above the riser (201).
2. The in-situ activation integrated treatment device for biomass hydrogenation catalyst according to claim 1, characterized in that, The reactor body (1) also includes a settling section (102) disposed on the upper part of the reactor shell (101). The diameter of the settling section (102) is larger than the diameter of the lower part of the reactor shell (101). The top of the top cover (103) is connected to an exhaust pipe (105), which is connected to the gas-solid separation component (4).
3. The in-situ activation integrated treatment device for biomass hydrogenation catalyst according to claim 1, characterized in that, The mixing and inhalation chamber (301) has an inverted trumpet-shaped or cylindrical structure. The bottom of the mixing and inhalation chamber (301) is connected to several support legs (302). The support legs (302) are supported on the top of the bottom end cap (104), so that an inhalation gap for the catalyst to pass through is formed between the bottom edge of the mixing and inhalation chamber (301) and the bottom end cap (104).
4. The in-situ activation integrated treatment device for biomass hydrogenation catalyst according to claim 1, characterized in that, The reflux assembly (2) also includes several positioning ribs (203) connected between the inner wall of the riser pipe (201) and the outer wall of the central return gas pipe (202), the central return gas pipe (202) being used to transport the gas from the upper part of the reactor downward to the mixing and inhalation chamber (301).
5. The in-situ activation integrated treatment device for biomass hydrogenation catalyst according to claim 1, characterized in that, The reflux assembly (2) also includes a reflux gas collection hood (204) disposed above the outlet of the riser pipe (201). The reflux gas collection hood (204) is in the shape of an inverted funnel, and its lower end is sealed to the upper opening of the central reflux pipe (202).
6. The in-situ activation integrated treatment device for biomass hydrogenation catalyst according to claim 5, characterized in that, The reflux assembly (2) also includes a filter screen (205) covering the upper opening of the reflux gas collection hood (204) for filtering the gas entering the central reflux pipe (202).
7. The in-situ activation integrated treatment device for biomass hydrogenation catalyst according to claim 2, characterized in that, The top of the cyclone separator (401) is provided with an air riser pipe (402), which is connected to the exhaust pipe (105). The bottom of the cyclone separator (401) is connected to a downwardly extending material leg (403).
8. The in-situ activation integrated treatment device for biomass hydrogenation catalyst according to claim 7, characterized in that, The end of the feed leg (403) is provided with a one-way valve (404), which is configured to prevent the gas in the annular activation zone (5) from flowing back into the cyclone separator (401).
9. The in-situ activation integrated treatment device for biomass hydrogenation catalyst according to claim 1, characterized in that, The annular activation zone (5) is provided with baffles (6), which are fixed alternately on the inner wall of the reactor shell (101) and the outer wall of the riser pipe (201).
10. An integrated in-situ activation method for a biomass hydrogenation catalyst, applied to an integrated in-situ activation device for a biomass hydrogenation catalyst according to any one of claims 1-9, characterized in that, Includes the following steps: S1 Raw material injection and mixing: The biomass raw material is brought to the nozzle (304) through the feed pipe (303) of the feed assembly (3) and sprayed upward. A negative pressure is formed in the mixing and suction chamber (301), and the catalyst outside the mixing and suction chamber (301) is sucked in through the gap between the support legs (302). The sucked catalyst is mixed with the raw material and the high temperature return gas from the central return gas pipe (202) to form a gas-solid mixture. S2 reaction and heat exchange: The gas-solid mixture flows upward into the riser (201) of the reflux assembly (2) and undergoes a hydrogenation reaction. At the same time, the high-temperature reflux gas flows downward in the central return gas pipe (202) and transfers heat to the fluid in the riser (201) through the pipe wall. S3 Gas-solid separation: The gas-solid mixture after the reaction undergoes initial settling in the settling section (102), and then enters the cyclone separator (401) of the gas-solid separation component (4). The separated gas flows into the exhaust pipe (105) through the riser pipe (402) and is discharged. The separated catalyst falls back down through the material leg (403) opening the one-way valve (404). S4 In-situ activation and regeneration: The catalyst falls back to the annular activation zone (5), is disturbed by the baffle (6) during the fall, and is stripped by the gas flowing upward in the annular activation zone (5) in the countercurrent direction. After completing the in-situ activation, it settles to the bottom and participates in the cycle of step one again. S5 Gas Reflux Circulation: A portion of the high-temperature product gas is captured by the reflux gas collection hood (204). After being filtered by the filter screen (205), the gas enters the central return gas pipe (202) and flows downwards.